Method and device for the low-temperature separation of air at variable energy consumption

• US 10,215,489 B2
• Filed: 06/25/2015
• Issued: 02/26/2019
• Est. Priority Date: 07/05/2014
• Status: Active Grant

• Current Assignee: Linde AG (Linde Plc)
• Original Assignee: Linde AG (Linde Plc)
• Inventors: Golubev, Dimitri
• Primary Examiner(s): King, Brian M
• Application Number:
  US15/322,740
• Publication Number:
  US 20170153058A1
• Time in Patent Office: 1,342 Days
• CPC Class Codes: F25J 2205/04 in the feed line, i.e. upstream of the fractionation step
• CPC Class Codes: F25J 2240/42 the fluid being air
• CPC Class Codes: F25J 2245/50 the recycled stream being oxygen
• CPC Class Codes: F25J 3/04018 of main feed air
• CPC Class Codes: F25J 3/04024 of purified feed air, so-called boosted air
• CPC Class Codes: F25J 3/0403 of nitrogen
• CPC Class Codes: F25J 3/04054 of air
• CPC Class Codes: F25J 3/04084 of nitrogen
• CPC Class Codes: F25J 3/0409 of oxygen
• CPC Class Codes: F25J 3/04175 at a pressure of substantially more than the highest pressure column
• CPC Class Codes: F25J 3/042 having an intermediate feed connection
• CPC Class Codes: F25J 3/0429 of feed air, e.g. used as waste or product air or expanded into an auxiliary column
• CPC Class Codes: F25J 3/04296 Claude expansion, i.e. expanded into the main or high pressure column
• CPC Class Codes: F25J 3/04345 and comprising a gas work expansion loop
• CPC Class Codes: F25J 3/04393 using multiple or multistage gas work expansion
• CPC Class Codes: F25J 3/04412 in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
• CPC Class Codes: F25J 3/04678 cooled by oxygen enriched liquid from high pressure column bottoms
• CPC Class Codes: F25J 3/04721 Producing pure argon, e.g. recovered from a crude argon column
• CPC Class Codes: F25J 3/04812 Different modes, i.e. "runs" of operation F25J3/04472 takes precedence

Abstract

A method and a device used to variably obtain a compressed-gas product by means of the low-temperature separation of air in a distillation column system. In a first operating mode, a first amount of first compressed-gas product is obtained, and, in a second operating mode, a second, smaller amount is obtained. In the first operating mode, a first amount of high-pressure column nitrogen is compressed in a nitrogen compressor and in the second operating mode, a second, larger amount is compressed in the nitrogen compressor.

Claims

1. A method for variably obtaining a pressurized-gas by means of low-temperature separation of air in a distillation column system comprising a high-pressure column and a low-pressure column, said method comprising:

compressing the entire feed air in a main air compressor to a first pressure, which is at least 4 bar higher than an operating pressure of the high-pressure column,

cooling a first partial stream of the feed air compressed in the main air compressor to a first intermediate temperature in a main heat exchanger, and work expanding the first partial stream in a first air turbine to form an expanded first partial stream,

introducing at least a first part of the expanded first partial stream into the distillation column system,

further compressing a second partial stream of the feed air compressed in the main air compressor to a second pressure, which is higher than the first pressure, in a first booster air compressor driven by the first turbine, cooling the second partial stream in the main heat exchanger, and subsequently expanding the second partial stream and introducing the expanded second partial stream into the distillation column system,

removing a first product stream in liquid form from the distillation column system and increasing the pressure of the first product stream to a first product pressure,

evaporating or pseudo-evaporating and warming the first product stream in the main heat exchanger,

obtaining warmed first product stream as a first pressurized-gas product,

compressing a first process stream, containing at least 78 mol % of nitrogen, in a multi-stage compressor from an inlet pressure to a final pressure,

wherein the multi-stage compressor is a nitrogen product compressor and

wherein the first process stream is a first gaseous nitrogen stream from the low-pressure column,

said method further comprising

in said first operating mode, obtaining a first amount of said first pressurized-gas product,

in said second operating mode, obtaining a second amount of said first pressurized-gas product, which is smaller than the first amount first pressurized-gas product,

in the first operating mode, obtaining a second process stream which is a first gaseous stream from the high-pressure column and contains at least 78 mol % of nitrogen, and wherein no amount or a first amount of the second process stream is mixed with the first process stream downstream of a first stage of the multi-stage compressor and, with the first process stream, is compressed in the multi-stage compressor, and

in the second operating mode, a second amount of the second process stream is compressed in the multi-stage compressor, wherein said second amount of the second process stream is greater than the amount of the second process stream compressed in the multi-stage compressor in said first operating mode.

2. The method as claimed in claim 1, wherein in the first operating mode, said first amount of the second process stream is mixed with the first process stream.

3. The method as claimed in claim 1, further comprising, in the second operating mode, removing an oxygen gas stream from a lower region of the low-pressure column, mixing the oxygen gas stream with a nitrogen-enriched stream from an upper region of the low-pressure column to form a mixture, and warming the mixture in the main heat exchanger.

4. The method as claimed in claim 1, wherein before said cooling and expanding of the second partial stream, the second partial stream is cooled in the main heat exchanger to a second intermediate temperature in the main heat exchanger, the second partial stream is then further compressed to a third pressure, which is higher than the first pressure, in a second booster air compressor, which is operated as a cold compressor and is driven by the second turbine, and then the second partial stream is introduced into the main heat exchanger at a third intermediate temperature and cooled in the main heat exchanger, expanded, and introduced into the distillation column system.

5. The method as claimed in claim 4, further comprising

cooling a third partial stream of the feed air compressed in the main air compressor to a fourth intermediate temperature in the main heat exchanger and work-expanding the third partial stream in a second air turbine to form an expanded third partial stream, and

introducing at least part of the expanded third partial stream into the distillation column system.

6. The method as claimed in claim 5, wherein a fourth partial stream of the feed air compressed in the main air compressor is cooled under the first pressure in the main heat exchanger, expanded and introduced into the distillation column system.

7. The method as claimed in claim 6, wherein

the third partial stream is work-expanded in the second air turbine to a pressure that is at least one bar higher than an operating pressure of the high-pressure column, and

before the at least part of the third partial stream is introduced into the distillation column system, the expanded third partial stream is further cooled in the main heat exchanger and subsequently expanded.

8. The method as claimed in claim 1, wherein

in the first operating mode, a first amount of feed air is compressed in the main air compressor and

in the second operating mode, a second amount of feed air is compressed in the main air compressor, and

wherein the ratio of the second amount of feed air to the first amount of feed air is, greater than the ratio between the second amount of first pressurized-gas product and the first amount of first pressurized-gas product.

9. The method as claimed in claim 1, wherein the first partial stream of the feed air compressed in the main air compressor is further compressed, upstream of the main heat exchanger, in said first booster air compressor.

11. The method according to claim 5, wherein the inlet pressure of the second air turbine is equal to the first pressure.

12. The method according to claim 5, wherein said third partial stream of the feed air is introduced into the main heat exchanger at the first pressure.

13. The method according to claim 5, wherein a fourth partial stream of the feed air compressed in the main air compressor is cooled under the first pressure in the main heat exchanger, expanded and introduced into the distillation column system.

14. The method according to claim 1, wherein

in the first operating mode, a first amount of feed air is compressed in the main air compressor,

in the second operating mode, a second amount of feed air is compressed in the main air compressor, and

wherein the ratio of the second amount of feed air to the first amount of feed air is at least 3% greater than the ratio between the second amount of first pressurized-gas product and the first amount of first pressurized-gas product.

15. The method according to in claim 14, wherein the ratio of the second amount of feed air to the first amount of feed air is more than 5% greater than the ratio between the second amount of first pressurized-gas product and the first amount of first pressurized-gas product.

16. The method according to in claim 1, wherein the first pressure is 6 to 16 bar, higher than said operating pressure of the high-pressure column.

17. The method according to claim 1, wherein the first pressure is between 17 and 25 bar.

18. The method according to claim 4, wherein the second intermediate temperature is higher than the first intermediate temperature.

19. The method according to claim 4, wherein the third intermediate temperature is higher than the second intermediate temperature.

20. The method according to claim 18, wherein the third intermediate temperature is higher than the second intermediate temperature.

21. The method according to claim 5, wherein the fourth intermediate temperature is lower than the first intermediate temperature.

10. A device for variably obtaining a pressurized-gas by low-temperature separation of air, said device comprising:

a distillation column system having a high-pressure column and a low-pressure column,

a main air compressor for compressing the entire feed air to a first pressure, which is at least 4 bar higher than an operating pressure of the high-pressure column,

a main heat exchanger,

means within the main heat exchanger for cooling down a first partial stream of the feed air compressed in the main air compressor to an intermediate temperature,

a first air turbine for work-expanding the first partial stream removed from the main heat exchanger,

means for introducing the expanded first partial stream into the distillation column system,

a first booster air compressor for further compressing a second partial stream of the feed air compressed in the main air compressor to a second pressure, which is higher than the first pressure, wherein the first booster air compressor is driven by the first turbine, is recompressed,

means in the main heat exchanger for cooling the further compressed second partial stream,

means for expanding the second partial stream removed from the main heat exchanger, and introducing the second partial stream into the distillation column system,

means for removing a first product stream in liquid form from the distillation column system, and means for increasing the pressure of the first product stream to a first product pressure,

means in the main heat exchanger for evaporating or pseudo-evaporating and warming the first product stream under the first product pressure,

means for obtaining the first product stream as a first pressurized-gas product,

a multi-stage compressor for compressing a first process stream, containing at least 78 mol % of nitrogen, from an inlet pressure to a final pressure,

wherein the multi-stage compressor is a nitrogen product compressor and

wherein the first process stream is a first gaseous nitrogen stream from the low-pressure column,

means for mixing a second process stream, containing at least 78 mol % of nitrogen, with the first process stream downstream of the first stage of the multi-stage compressor, wherein the second process stream is a first gaseous nitrogen stream from the high-pressure column,

means for switching over between a first operating mode and a second operating mode,

wherein in the first operating mode, a first amount of first pressurized-gas product is obtained,

wherein in a second operating mode, a second amount of first pressurized-gas product, which is smaller than the first amount, is obtained and

the means for switching over between the first operating mode and the second operating mode permitting

in the first operating mode, compressing no amount or a first amount of the second process stream in the multi-stage compressor from an inlet pressure to a final pressure and

in the second operating mode, compressing a second amount of the second process stream, which is greater than the amount of the second process stream compressed in the first operating mode, in the multi-stage compressor.